EP2414097A2 - Improved aqueous phase oxidation process - Google Patents

Improved aqueous phase oxidation process

Info

Publication number
EP2414097A2
EP2414097A2 EP10711122A EP10711122A EP2414097A2 EP 2414097 A2 EP2414097 A2 EP 2414097A2 EP 10711122 A EP10711122 A EP 10711122A EP 10711122 A EP10711122 A EP 10711122A EP 2414097 A2 EP2414097 A2 EP 2414097A2
Authority
EP
European Patent Office
Prior art keywords
reactor
feedstock
reaction mixture
approximately
oxygen gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP10711122A
Other languages
German (de)
English (en)
French (fr)
Inventor
George G. Foster
Frederick P. Kesler
Malcolm Draper
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Earth Renewal Group LLC
Original Assignee
Earth Renewal Group LLC
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from US12/416,412 external-priority patent/US7951988B2/en
Priority claimed from US12/416,424 external-priority patent/US7915474B2/en
Priority claimed from US12/416,419 external-priority patent/US8115047B2/en
Priority claimed from US12/416,431 external-priority patent/US8481800B2/en
Priority claimed from US12/416,438 external-priority patent/US8168847B2/en
Application filed by Earth Renewal Group LLC filed Critical Earth Renewal Group LLC
Publication of EP2414097A2 publication Critical patent/EP2414097A2/en
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/727—Treatment of water, waste water, or sewage by oxidation using pure oxygen or oxygen rich gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/06—Treatment of sludge; Devices therefor by oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/005—Processes using a programmable logic controller [PLC]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/02—Temperature
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/03—Pressure
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/05—Conductivity or salinity
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH

Definitions

  • the process used a significant amount of oxygen gas to oxidize the reduction products of nitric acid.
  • the oxygen gas was initially bubbled into the aqueous phase but quickly separated and collected in the headspace of the reactor where it was eventually removed. It was necessary to supply a large amount of oxygen gas to adequately oxygenate the aqueous phase.
  • a number of embodiments of an improved aqueous phase oxidation process are described below.
  • the improved process reduces or eliminates many of the problems and disadvantages associated with conventional aqueous phase oxidation processes.
  • the process can be used to oxidize any suitable organic or inorganic feedstock.
  • the process is used to oxidize municipal and/or farm waste, e.g., dcwatered sewage, municipal sludge cake, or animal manure.
  • the feedstock is oxidized in an aqueous reaction mixture by one or more oxidizing acids.
  • the oxidizing acid is regenerated in situ.
  • Oxygen gas may be supplied to the reaction mixture to reoxidize the reduction products of the oxidizing acid.
  • the reactor may be maintained at suitable pressures and temperatures to facilitate regeneration of the oxidizing acid.
  • Suitable oxidizing acids that may be used in the process include nitric acid and sulfuric acid.
  • the feedstock may be processed before being fed to the reactor to give it uniform physical properties and to render it better suited to be rapidly and efficiently oxidized.
  • This processing may include comminuting the feedstock so that the particles have a uniform size that allows the feedstock to easily enter the reactor, combining the feedstock with recycled effluent from the reactor, and/or combining the feedstock with one or more oxidizing acids before the feedstock enters the reactor.
  • gas from the headspac ⁇ of the reactor in particular, oxygen gas
  • gas from the headspac ⁇ of the reactor is dispersed into the reaction mixture, This may be accomplished with a hollow impeller that causes gas from the headspace to flow through the impeller and into the reaction mixture as the impeller rotates.
  • the composition of the gas in the reaction mixture is close to or the same as the composition of the gas in the headspace.
  • concentration of oxygen gas in the dissolved and undissolvcd gas portion of the reaction mixture is similar, if not the same, as the
  • the reaction mixture may be mixed vigorously to increase the total amount of oxygen gas the enters the mixture,
  • the gas in the reaction mixture may be removed as part of the liquid effluent stream.
  • the gas that is dissolved and undissolved in the reaction mixture is removed with the reaction mixture effluent,
  • a separate gas removal port on the reactor is unnecessary, but may be provided for other purposes.
  • the effluent exits the reactor, it is cooled and the pressure is reduced to allow the gas to separate.
  • the effluent may be vigorously agitated to speed up the separation and make it more complete.
  • a portion of the effluent may be recycled back to the beginning of the process and combined with the feedstock as mentioned above.
  • the initial feedstock is combined with either or both of the effluent from the reactor or one or more oxidizing acids to form a primary feedstock.
  • the primary feedstock is fed into the reactor where it is oxidized.
  • the primary feedstock is part of the reaction mixture which also includes nitric acid and a secondary oxidizing acid.
  • the initial feedstock is combined with either or both of the effluent from the reactor or one or more oxidizing acids to form the primary feedstock.
  • the primary feedstock is fed into the reactor where it is oxidized.
  • the primary feedstock is part of the reaction mixture which also includes nitric acid and oxygen gas.
  • the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid.
  • the reaction mixture is maintained at a temperature that is no more than approximately 210 0 C.
  • the initial feedstock is combined with either or both of the effluent from the reactor or one or more oxidizing acids to form the primary feedstock.
  • the primary feedstock is oxidized in the reactor.
  • the primary feedstock is part of the reaction mixture which also includes nitric acid.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the initial feedstock is combined with either or both of the effluent from the reactor or one or more oxidizing acids to form the primary feedstock.
  • the primary feedstock is oxidized in the reactor.
  • the primary feedstock is part of the reaction mixture which also includes nitric acid, a secondary oxidizing acid, and oxygen gas.
  • the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid.
  • the reaction mixture is maintained at a temperature that is no more than approximately 210 0 C.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the initial feedstock is comminuted to form the primary feedstock where the largest dimension of at least approximately 95% of the particles in the primary feedstock is no more than 7 mm.
  • the primary feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid and the secondary oxidizing acid.
  • the initial feedstock is comminuted to form the primary feedstock where the largest dimension of at least approximately 95% of the particles in the primary feedstock is no more than 7 mm.
  • the primary feedstock is oxidized in the reactor where it is part of die reaction mixture which also includes nitric acid and oxygen gas.
  • the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid.
  • the temperature of the reaction mixture is maintained at no more than approximately 210 0 C.
  • the initial feedstock is comminuted to form the primary feedstock where the largest dimension of at least approximately 95% of the particles in the primary feedstock is no more than 7 mm.
  • the primary feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the initial feedstock is comminuted to form the primary feedstock where the largest dimension of at least approximately 95% of the particles in the primary feedstock is no more than 7 mm.
  • the primary feedstock is fed into the reactor at an approximately constant feed rate and oxidized.
  • the primary feedstock is part of the reaction
  • the mixture which also includes nitric acid, a secondary oxidizing acid, and oxygen gas.
  • the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid.
  • the temperature of the reaction mixture is maintained at no more than approximately 210 0 C.
  • the pressure in the reactor is maintained at at least approximately kPa,
  • the feedstock is fed into the reactor at a feed rate that is approximately constant.
  • the feedstock is oxidized in the reactor where it is part the reaction mixture which also includes nitric acid and a secondary oxidizing acid.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the feed rate is approximately constant even though the pressure in the reactor may vary from approximately 2070 kPa to 6,900 kPa.
  • the feedstock is fed into the reactor by a feeding device that is powered hydraulicly or by a gearmotor.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid and a secondary oxidizing acid.
  • a first amount of the feedstock is fed into the pressurized reactor by the feeding device.
  • the feeding device is isolated from the pressurized reactor and filled with a second amount of the feedstock.
  • the second amount of the feedstock is fed into the pressurized reactor by the feeding device.
  • the feedstock is oxidized in the pressurized reactor where it is part of the reaction mixture which also includes nitric acid and a secondary oxidizing acid.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the feedstock is fed into the reactor at a feed rate that is approximately constant.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid, a secondary oxidizing acid, and oxygen gas.
  • the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid.
  • the temperature of the reaction mixture is maintained at no more than approximately 210 0 C.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the feed rate is approximately constant even though the pressure in the reactor may vary from approximately 2070 kPa to 6,900 kPa.
  • the feedstock is fed into the reactor at a feed rale that fluctuates no more than approximately 10% per hour.
  • the feedstock is oxidized in a reactor where it is part of the reaction mixture which also includes nitric acid,
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the feed rate fluctuates no more than approximately 10% per hour even though the pressure in the reactor may vary from approximately 2070 kPa to 6,900 kPa.
  • the feedstock is fed into the reactor with a feeding device that is powered hydraulicly or by a gcarmotor.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid and oxygen gas.
  • the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid.
  • the temperature of the reaction mixture is maintained at no more than approximately 210 °C.
  • the feedstock is fed into the reactor with a feeding device that is powered hydraulicly or by a gearmotor.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa,
  • the feedstock is fed into the reactor with a feeding device that is powered hydraulicly or by a gearmotor.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid, a secondary oxidizing acid, and oxygen gas.
  • the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid.
  • the temperature of the reaction mixture is maintained at no more than approximately 210 0 C.
  • the pressure of the reactor is maintained at at least approximately 2070 kPa,
  • a first amount of the feedstock is fed into a pressurized reactor by the feeding device.
  • the feeding device is isolated from the pressurized reactor and filled with a second amount of the feedstock.
  • the second amount of the feedstock is fed into the pressurized reactor by the feeding device.
  • the feedstock is oxidized in the pressurized reactor where it is part of the reaction mixture that also includes nitric acid. The pressure in the
  • pressurized reactor is maintained at at least approximately 2070 kPa.
  • the first amount of the feedstock and the second amount of the feedstock are fed into the pressurized reactor at a feed rate that fluctuates no more than approximately 10% per hour,
  • a first amount of the feedstock is fed into the pressurized reactor by the feeding device.
  • the feeding device is isolated from the pressurized reactor and filled with a second amount of die feedstock.
  • the second amount of the feedstock is fed into the pressurized reactor by the feeding device.
  • the feedstock is oxidized in the pressurized reactor where it is part of the reaction mixture that also includes nitric acid, a secondary oxidizing acid, and oxygen gas.
  • the temperature of the reaction mixture is maintained at no more than approximately 210 °C.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the first amount of the feedstock and the second amount of the feedstock are fed into the pressurized reactor at a feed rate that is approximately constant.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid and a secondary oxidizing acid.
  • the gas from the headspace of the reactor is dispersed into the reaction mixture.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid and oxygen gas.
  • the oxygen gas is supplied to the reactor and dispersed from the headspace into the reaction mixture in a manner that is sufficient to regenerate at least a majority of the nitric acid.
  • the temperature of the reaction mixture is maintained at no more than approximately 210 °C.
  • the feedstock is oxidized in a reactor where it is part of the reaction mixture which also includes nitric acid and a secondary oxidizing acid.
  • concentration of dissolved and imdissolved oxygen gas in the gaseous portion of the reaction mixture is maintained within approximately 25% of the concentration of oxygen gas in a headspace of the reactor.
  • the feedstock is oxidized in a reactor where it is part of the reaction mixture which also includes nitric acid, a secondary oxidizing acid, and oxygen gas.
  • the oxygen gas is supplied to the reactor and dispersed from the headspace of the reactor into
  • the reaction mixture in a manner that is sufficient to regenerate at least a majority of the nitric acid.
  • the temperature of the reaction mixture was maintained at no more than approximately 210 0 C.
  • the pressure in the reactor was maintained at at least approximately 2070 kPa.
  • the feedstock is oxidized in a reactor where it is part of the reaction mixture which also includes nitric acid. Gas from the headspace of the reactor is dispersed into the reaction mixture. The pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid arid oxygen gas.
  • the oxygen gas is supplied to the reactor mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid.
  • the concentration of dissolved and undissolved oxygen gas in the gaseous portion of the reaction mixture is maintained within approximately 25% of the concentration of oxygen gas in the headspace of the reactor.
  • the temperature of the reaction mixture is maintained at no more than approximately 210 0 C.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid.
  • concentration of dissolved and undissolved oxygen gas in the gaseous portion of the reaction mixture is maintained within approximately 25% of the concentration of oxygen gas in the headspace of the reactor.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid, a secondary oxidizing acid, and oxygen gas.
  • the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid.
  • the concentration of dissolved and undissolved oxygen gas in the gaseous portion of the reaction mixture is maintained within approximately 25% of the concentration of oxygen gas in the headspace of the reactor.
  • the temperature of the reaction mixture is maintained at no more than approximately 210 0 C.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid and a secondary oxidizing acid.
  • Gas is supplied to the reactor, and reactor effluent is removed from the reactor, Also, at least approximately 94 wt. % of the reaction mixture that exits the reactor does so in the reactor effluent, and at least approximately 94 wt.% of gas that exits the reactor does so in the reactor effluent.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid and oxygen gas.
  • Gas including oxygen gas, is supplied to the reactor.
  • the reactor effluent is removed from the reactor.
  • the temperature of the reaction mixture is maintained at no more than approximately 210 0 C?.
  • the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid Also, at least approximately 94 wt.% of the reaction mixture that exits the reactor does so in the reactor effluent, and at least approximately 94 wt.% of gas that exits the reactor does so in the reactor effluent,
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid and a secondary oxidizing acid.
  • Oxygen gas is supplied to the reactor, and the reactor effluent is removed from the reactor.
  • the amount of oxygen gas in the reactor effluent is measured and the supply of oxygen gas to the reactor is adjusted based on the amount of oxygen gas measured in the reactor effluent.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid, a secondary oxidizing acid, and oxygen gas.
  • Gas, including oxygen gas, is supplied to the reactor.
  • Reactor effluent is removed from the reactor.
  • the temperature of the reaction mixture is maintained at no more than approximately 210 0 C.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid, Also, at least approximately 94 wt.% of the reaction mixture that exits the reactor does so in the reactor effluent, and at least approximately 94 wt.% of gas that exits the reactor does so in the reactor effluent.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid.
  • Gas is supplied to the reactor, and the reactor effluent is removed from the reactor.
  • the pressure in die reactor is maintained at at least approximately 2070 kPa. Also, at least approximately 94 wt.% of the reaction mixture that exits the reactor docs so in the reactor effluent, at least approximately 94 wt.% of gas that exits the reactor does so in the reactor effluent.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid and oxygen gas.
  • the oxygen gas is supplied to the reactor in an amount that is sufficient to regenerate at least a majority of the nitric acid.
  • the reactor effluent is removed from the reactor. The amount of oxygen gas in the reactor effluent is measured and the supply of oxygen gas is adjusted accordingly, The temperature of the reaction mixture is maintained at no more than approximately 210 0 C.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid.
  • Gas is supplied to the reactor, and the reactor effluent is removed from the reactor.
  • the amount of oxygen gas in the reactor effluent is measured and the supply of oxygen gas is adjusted accordingly.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the feedstock is oxidized in the reactor where it is part of the reaction mixture which also includes nitric acid, a secondary oxidizing acid, and oxygen gas.
  • the oxygen gas is supplied to the reactor, and the reactor effluent is removed from the reactor.
  • the amount of oxygen gas in the reactor effluent is measured and the supply of oxygen gas is adjusted accordingly.
  • the temperature of the reaction mixture is maintained at no more than approximately 210 0 C.
  • the pressure in the reactor is maintained at at least approximately 2070 kPa.
  • the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid.
  • FIG. 1 is a block diagram of an improved aqueous phase oxidation process thai includes a feedstock processing system, a reaction system, and an effluent processing system.
  • Figure 2 is a block diagram of one embodiment of the feedstock processing system from Figure 1.
  • FIG. 3 is a block diagram of another embodiment of the feedstock processing system from Figure 1.
  • Figure 4 is a block diagram of one embodiment of the reaction system from Figure 1.
  • FIG. 5 is a block diagram of one embodiment of the effluent processing system from Figure 1.
  • the improved oxidation process in its various embodiments, can be used to oxidize a wide variety of materials.
  • the process can be used to oxidize organic and/or inorganic material with very similar results in the sense that the feed material is completely or nearly completely oxidized, although the reaction products may be very different.
  • Specific materials that may be oxidized using this process include, but are not limited to, municipal and farm waste including dewat ⁇ red sewage, municipal sludge cake and animal manure; slaughter house waste that includes blood, bone, and flesh; petroleum based wastes such as plastics, rubber, and paints; tires; wood pulp; hazardous materials such as nerve gas, municipal garbage, and metal ore such as sulfide containing ores that are typically processed in smelters.
  • the process 100 includes a feedstock processing system 104, a reaction system 106, and an effluent processing systenilO ⁇ .
  • the raw feedstock 102 enters the feedstock processing system 104 where it is modified and/or processed in a number of ways to produce a primary feedstock.
  • the primary feedstock is fed to the reaction system 106 where it is oxidized.
  • the effluent from the reaction system 106 enters the effluent processing system 108 where it is separated and/or otherwise processed to produce final products 110.
  • Each system 104, 106, 108 is described in greater detail.
  • the raw feedstock 102 may be any suitable feedstock that is capable of being oxidized in the manner described herein,
  • the feedstock is a sewage or manure based material that is approximately 3% to 20% solids (e.g., 18% solids).
  • FIG. 2 shows a block diagram of one embodiment of the feedstock processing system 200.
  • the raw feedstock 102 is initially mixed with recycled effluent 204 to form an intermediate feedstock.
  • the grinder 206 comminutes the intermediate feedstock ⁇ hereby forming
  • the recycled effluent 204 may be combined with the raw feedstock 102 in the grinder 206, as shown in Figure 2, or before entering the grinder 206. If they are combined in the grinder 206, the grinding action may serve to mix the two materials together. If they are combined before entering the grinder 206, the recycled effluent 204 arid the raw feedstock 102 may be mixed in a separate vessel.
  • the recycled effluent 204 is added in an amount that is sufficient to create a slurry that doesn't plug or clog the grinder 206 and/or facilitates later processing arid transport.
  • the amount of recycled effluent 204 that is added may vary depending on the characteristics of the raw feedstock 102, Generally, larger quantities of the recycled effluent 204 are used if the raw- feedstock 102 is dry, while smaller quantities, or possibly none at all, are used if the raw feedstock 102 already includes a suitable amount of liquid. It is also possible that certain feedstocks may be so wet that they must be de watered before entering the process 100.
  • the volume ratio of the recycled effluent 204 to the raw feedstock 102 in the intermediate feedstock may be approximately 0.5 to 1 .5 or, desirably, approximately 0.75 to 1.25. In one embodiment, approximately equal parts by volume of the recycled effluent 204 and the raw feedstock 102 are combined to form the intermediate feedstock.
  • the recycled effluent 204 may be supplied at an elevated temperature so that it heats the raw feedstock 102 when the two are mixed together.
  • the resulting intermediate feedstock may be significantly above ambient temperature.
  • the recycled effluent 204 may be supplied at a temperature of approximately 40 0 C to 90 0 C or, desirably, 50 0 C to 75 °C.
  • the intermediate feedstock may be approximately 37 °C to 50 0 C.
  • the effluent from reactor 402 ( Figure 4) is heated by the exothermic oxidation of the feedstock.
  • the recycled effluent 204 may be at an elevated temperature simply because it has not cooled (either naturally or actively cooled) after leaving the reactor 402.
  • the recycled effluent 204 may also be heated in a heat exchanger to
  • the recycled effluent 204 is heated in a heat exchanger using heat from the effluent that has just left the reactor 402.
  • the recycled effluent 204 may be stored in an insulated lank or vessel before being mixed with the raw feedstock 102 to maintain it at an elevated temperature.
  • the intermediate feedstock is comminuted to reduce the particle sizes, improve the uniformity of the feedstock, make the feedstock more amenable to evenly controlled pumping, and keep the solids suspended in the slurry. This makes it easier to feed the feedstock into the reactor 402, which is often operated at an elevated pressure, without plugging the entry opening.
  • the size and uniformity are also important because the reaction rate varies significantly based on these factors, especially particle size. Larger particles generally need longer residence times to completely oxidize. Tf the feedstock has both large and small particles, the large particles tend to dictate the residence time. Thus, it is desirable to create a feedstock that generally has small, uniform particles. This is especially true when the feedstock includes organic matter such as sewage and/or manure.
  • the largest dimension of at least approximately 95% of the particles in the comminuted feedstock is no more than 7 mm, no more than 4 mm, no more than 2.5 mm, desirably, no more than 1.5 mm, or, suitably, no more than 0.5 mm.
  • the largest dimension of at least approximately 98% of the particles in the comminuted feedstock is no more than 7 mm, no more than 4 mm, no more than 2.5 mm, desirably, no more than 1.5 mm, or, suitably, no more than 0.5 mm.
  • the largest dimension of at least substantially all of the particles in the comminuted feedstock is no more than 7 mm, no more than 4 mm, no more than 2.5 mm, desirably, no more than 1.5 mm, or, suitably, no more than 0.5 mm.
  • the comminuted feedstock moves from the grinder 206 to a mixing vessel 208 where it is combined with a primary oxidizing acid or first acid 210 and a
  • pre-treating the feedstock in this manner increases the rate of the redox reaction in the reactor 402, particularly for feedstock that includes organic matter such as sewage and/or manure.
  • the acids 210, 212 initiate de-lignination of the organic fibers and other organic matter in the primary feedstock. De-lignination is beneficial because it further reduces the size of the particles in the feedstock and exposes them to chemical attack in the reaction svstem 106.
  • de-Hgnination begins when the recycled effluent 204, which includes the acids 210, 212, is first combined with the raw feedstock 102.
  • dc-lignination is initiated when the recycled effluent 204 is combined with the raw feedstock 102 in the grinder 206 and accelerates when the additional acids 210, 212 are added in the vessel 208.
  • the primary oxidizing acid 210 and the secondary oxidizing acid 212 arc added until the concentration of the acids 210, 212 in the primary feedstock, excluding solids (i.e., the concentration of the primary feedstock excluding the solids portion), is approximately the same as the concentration of the acids 210, 212, respectively, in the reactor 402 at start-up.
  • the primary oxidizing acid 210 may be nitric acid, and the secondary oxidizing acid 212 may be sulfuric acid.
  • the nitric acid functions as the oxidizing agent to oxidize the feedstock.
  • the nitric acid is included in an amount that is sufficient to rapidly and completely oxidize the feedstock.
  • the sulfate ions of the sulfuric acid convert the salt forming reaction products into stable sulfate salts, thereby leaving the nitric acid in the acid state to continue as the primary oxidant.
  • the sulfate reacts with nitrogen containing compounds to prevent the formation of ammonium nitrate, an explosive, and/or other undesirable reaction products. Instead, the sulfate reacts with nitrogen compounds to form ammonium sulfate.
  • the sulfuric acid is provided in an
  • the nitric acid may be added to achieve a concentration in the primary feedstock, excluding solids, of at least approximately 0,08 rnol/L, desirably, at least approximately 0,5 mol/L, or, suitably, at least approximately 0.84 mol/L.
  • the nitric acid may be added to achieve a concentration in the primary feedstock, excluding solids, of no more than approximately 4.2 mol/L, desirably, no more than approximately 3.3 mol/L, or, suitably, no more than approximately 2.5 mol/L.
  • the nitric acid may be added to achieve a concentration in the primary feedstock, excluding solids, of approximately 0.08 mol/L to 4.2 mol/L, desirably, approximately 0.5 mol/L to 3.3 mol/L, or, suitably, approximately 0.84 mol/L to 2.5 mol/L.
  • the nitric acid may be added to achieve a concentration in the primary feedstock, excluding solids, of at least approximately 0.5 wt.%, desirably, at least approximately 3 wt.%, or, suitably, at least approximately 5 wt.%.
  • the nitric acid may be added to achieve a concentration in the primary feedstock, excluding solids, of no more than approximately 25 wt.%, desirably, no more than approximately 20 wt,%, or, suitably, no more than approximately 15 wt.%.
  • the nitric acid may be added Io achieve a concentration in the primary feedstock, excluding solids, of approximately 0.5 wt.% to 25 wt.%, desirably, approximately 3 wt.% to 20 wt.%, or, suitably, approximately 5 wt.% to 15 wt.%.
  • the sulfuric acid may be added to achieve a concentration in the primary 7 feedstock, excluding solids, of at least approximately 0,1 mol/L, desirably, at least approximately 0.12 mol/L, or, suitably, at least approximately 0.16 mol/L.
  • the sulfuric acid may be added to achieve a concentration in the primary feedstock, excluding solids, of no more than approximately 1 mol/L, desirably, no more than approximately 0.54 mol/L, or, suitably, no more than approximately 0.32 mol/L.
  • the sulfuric acid may be added to achieve a concentration in the primary 7 feedstock, excluding solids, of at least approximately 0,1 mol/L, desirably, at least approximately 0.12 mol/L, or, suitably, at least approximately 0.16 mol/L.
  • the sulfuric acid may be added to achieve a concentration in the primary feedstock, excluding solids, of no more than approximately 1 mol/L, desirably, no more than approximately 0.54 mol/L, or,
  • feedstock excluding solids, of approximately 0,1 niol/L to 1 mol/L, desirably, approximately 0,12 mol/L to 0.54 mol/L, or, suitably, approximately 0.16 mol/L to 0.32 moi/'L,
  • the sulfuric acid may be added to achieve a concentration in the primary feedstock, excluding solids, of at leas! approximately 0.9 wt.%, desirably, at least approximately 1.1 wt.%, or, suitably, at least approximately 1.5 wt.%.
  • the sulfuric acid may be added to achieve a concentration in the primary feedstock, excluding solids, of no more than approximately 10 wt.%, desirably, no more than approximately 5 wt.%, or, suitably, no more than approximately 3 wt.%.
  • the sulfuric acid may be added to achieve a concentration in the primary feedstock, excluding solids, of approximately 0.9 wt.% to 10 wt.%, desirably, approximately 1.1 wt.% to 5 wt.%, or, suitably, approximately 1.5 wt.% to 3 wt.%.
  • the mixing vessel 208 may be any suitable tank, pipe, or other vessel that is capable of holding and/or mixing the materials.
  • the mixing vessel 208 should be made of a material that is chemically resistant to the acids 210, 212. Suitable materials include plastic, stainless steel, titanium, or the like.
  • the grinder 206 and the mixing vessel 208 may ⁇ be combined together so that everything is comminuted and/or mixed in the same vessel,
  • the primary feedstock exits the mixing vessel 208 and is stored in a storage vessel or tank 214 before it is fed into the reactor 402.
  • the storage vessel 214 may be insulated to maintain the temperature of the primary feedstock and conserve energy. It should be noted that it is generally not desirable to store the primary feedstock for a long period of time before feeding it into the reactor 402. The presence of the acids 210, 212 may cause the primary feedstock to separate and the texture to change in a way that can make it difficult to feed into the reactor 402.
  • the primary feedstock is now prepared to be fed into the reactor 402. This is accomplished using one or more feeding devices 216.
  • the primary feedstock is transferred to the feeding device 216 via a low pressure pump and a combination of vacuum and gravity flow. It should be appreciated, however, that any suitable method may be used to transfer the primary feedstock to the feeding device 216.
  • the feeding device 216 is used to feed the primary feedstock into the reactor 402 at a steady rate. It has been discovered that relatively minor fluctuations in the feed rate can cause large fluctuations in the redox reaction. If the feed rate drops, the reactor 402 is starved and if the feed rate climbs, the reactor 402 is overfed.
  • the feeding device 216 may have any suitable configuration that allows it to feed the primary feedstock at a steady rate.
  • the feeding device 216 is actuated or powered hydraulicly.
  • the feeding device 216 may include one or more hydraulic rams that dispense or force the primary feedstock into the reactor 402.
  • One example of a suitable hydraulicly powered feeding device is a cycling ram pump.
  • the feeding device 216 is actuated or powered by a gearmotor.
  • the feeding device 216 includes a gcarmotor that turns a screw which, in turn, feeds the primary feedstock into the reactor 402.
  • the feeding device 216 may be configured so that pressure fluctuations in the reactor 402, even up to the reactor's safe operating pressure limit of approximately 13,800 kPa, do not significantly change the feed rate.
  • the feeding device 216 is an extruder and/or injector that is hydraulicly or gear actuated. Multiple feeding devices 216 may be used to provide an uninterrupted supply of the primary feedstock to the reactor 402. The multiple feeding devices 216 may be sequentially activated and refilled. When one feeding device 216 is injecting the feedstock into the reactor 402, another feeding 216 may be refilled with the primary feedstock. Also, the use of multiple feeding devices 216 is advantageous because it allows one or more devices 216 to be offline for maintenance or repairs while the remainder of the devices 216 provide a continuous supply of feedstock to the reactor 402.
  • the feeding device 216 may feed the primary feedstock into the reactor at a rate that fluctuates no more than approximately 10% per hour, desirably, no more than approximately 5% per hour, or, suitably no more than approximately 2% per hour. In another embodiment, the feeding device 216 feeds the primary feedstock into the reactor at a feed rate that is approximately constant. The feeding device 216 is capable of maintaining these feed rates even though the pressure in the reactor 402 may vary from approximately 2070 kPa to 6,900 kPa.
  • the feeding device 216 is exposed to the high pressure of the reactor 402 when it is feeding the primary feedstock into the reactor 402. However, the feeding device 216 is at a low pressure when it is filled with the primary feedstock from the storage vessel 214.
  • the valves 218, 220 may be used to selectively isolate the feeding device 216 from the reactor 402 during feeding and refilling operations.
  • the valve 218 is closed and the valve 220 is open when the feeding device 216 injects the primary feedstock into the reactor 402,
  • the valve 220 is closed and the valve 218 is open when the feeding device 216 is refilled with the primary feedstock,
  • valves 218, 220 may also be used to isolate the feeding device 216 so that it can be repaired while the reactor 402 remains in operation. Moreover, the valves 218, 220 can also prevent back flow from the reactor 402 into the feedstock processing system 104 during an overpressure event. It should be appreciated that although the valves 218, 220 are depicted as being separate from the feeding device 216, the valves 218, 220 may be provided as integral components of the feeding device 216.
  • a pressure release system 222 may be provided that allows the feeding device 216 to transition from a high pressure state to a low pressure state without causing undue wear on the components and/or blowback into the mixing vessel 208 when the valve 218 is opened.
  • the pressure release system may include a tank that is capable of absorbing excess pressure.
  • FIG. 3 shows a block diagram of another embodiment of a feedstock processing system 300. This embodiment is similar to the feedstock processing system 200 except that the raw feedstock does not enter a
  • the primary feedstock is not stored in a separate storage vessel
  • the feedstock processing system 300 may be suitable for situations where the raw feedstock 102 does riot need to be comminuted.
  • the raw feedstock 102 may already be uniform with small particles.
  • the mixing vessel 208 may function as a storage vessel so thai the primary feedstock is drawn from the mixing vessel 208 into the reactor 402. Numerous other changes to the feedstock processing system 104 are also contemplated.
  • the reaction system 400 includes the reactor 402, which receives the processed feedstock from the feedstock processing system 104.
  • the reactor 402 is in fluid communication with a make-up acid source 404, an oxygen gas source 406, a control gas source 408, and a recycled gas source 410.
  • the reactor 402 includes one or more sensors 412 and an impeller or dispersion device 414.
  • the temperature of the reactor 402 may be controlled by an energy control system 416.
  • the reactor 402 is initially charged with an initial reaction mixture that includes an aqueous solution of the primary oxidizing acid and the secondary oxidizing acid.
  • the primary oxidizing acid is nitric acid and the secondary oxidizing acid is sulfuric acid.
  • the reactor 402 may be initially charged with an aqueous mixture of nitric and sulfuric acid having any of the concentrations described above. For example, equal volumes of approximately 3.35 mol/L nitric acid and 0.4 mol/L sulfuric acid may be combined in the reactor 402 to form the initial reaction mixture,
  • the reactor 402 may be filled to any suitable level with the initial reaction mixture.
  • the initial reaction mixture occupies at least approximately 25% of the volume of the reactor 402 or, suitably, at least approximately 35% of the volume of the reactor.
  • the initial reaction mixture occupies no more than approximately 80% of the volume of the reactor 402 or, suitably, no more than approximately 70% of the volume of the reactor 402.
  • the initial reaction mixture occupies approximately 25% to 80% of the volume of the reactor 402 or, suitably, approximately 35% to 70% of the
  • the initial reaction mixture occupies approximately 50% of the volume of the reactor 402.
  • the remainder of the volume of the reactor 402, i.e., the headspace, is occupied by gases.
  • the headspace is initially charged with oxygen gas and/or one or more other gases, preferably inert gases.
  • the oxygen gas is used to regenerate the nitric acid in the reaction mixture as described in greater detail below.
  • the oxygen gas 406 may be supplied from any suitable source.
  • the oxygen source may be air, pure oxygen, or even a product of another reaction.
  • the gas in the headspace at start-up includes at least approximately 2 volume percent oxygen gas, desirably, at least approximately 5 volume percent, or, suitably, at least approximately 8 volume percent.
  • the gas in the headspace at start-up includes no more than approximately 60 volume percent oxygen gas, desirably, no more than approximately 45 volume percent oxygen gas, or, suitably, no more than approximately 35 volume percent oxygen gas.
  • the gas in the headspace at start-up includes approximately 2 to 60 volume percent oxygen gas, desirably, 5 to 45 volume percent oxygen gas, or, suitably, 8 to 35 volume percent oxygen gas.
  • Suitable gases include nitrogen, argon, and the like. These gases are supplied as the control gas 408 in Figure 4.
  • the temperature and pressure are increased together until operating conditions arc reached. For example, when the temperature reaches 60 °C, the pressure is increased (by adding gas to the headspace) to approximately 1035 kPa. At 150 °C, the pressure is increased to approximately 2070 kPa. Once the mixture reaches operating temperature, the pressure is increased to approximately 3450 kPa. It should be appreciated, that the temperature and pressure may fluctuate substantially from the initial levels during processing.
  • the initial reaction mixture is heated by the energy control system to at least 150 °C as the impeller 414 vigorously mixes or agitates the reaction mixture.
  • the reactor 402 may be heated using a heat exchanger in the energy control system 416 that is in fluid communication
  • the reactor 402 may include an internal cooling coil that is used to maintain the temperature of the reaction mixture below a maximum threshold. It should be appreciated that the same coil may be used to heat and cool the reactor 402, if desired.
  • the energy control system 416 can be viewed as a collection of any number, type, or configuration of heat exchangers, heat sources, heat sinks and other energy transfer devices and components that can be used to add and/or extract heat from various streams, reactors, etc.
  • the energy control system 416 may include a supplemental heat source that is used to supply and/or remove heat from the heat exchanger using one or more heat exchange coils. Numerous other examples are also contemplated.
  • the impeller 414 is used to thoroughly and vigorously mix the reaction mixture and disperse the gas from the headspace into the reaction mixture.
  • the impeller 414 may have any suitable design or configuration so long as it is capable of adequately doing these things.
  • the impeller may be a gas enlrainment impeller.
  • the gas is dispersed by impeller blades attached to a hollow shaft through which gases are continuously recirculated from the headspace of the reactor 402, The gas enters openings near the top of the shaft and is expelled through dispersion ports located at the tips of the impeller blades.
  • the high speed rotation of the impeller blades creates a low pressure area at the tip.
  • the pressure at the tip of the blades drops as the speed of the impeller 414 increases, thereby increasing the rate at which gas is dispersed from the headspace through the reaction mixture.
  • the reactor 402 may also include one or more baffles that enhance dispersion of the headspace gas as well as the general stirring of the reaction mixture.
  • the transfer of gas is governed by the relative speed of the tips of the impeller 414 to the liquid phase, which reduces the pressure at the tips (i.e., creates a vacuum) of the impeller 414 and thereby draws gas into the reaction mixture.
  • a baffle may be used to impede rotation of the liquid reaction mixture relative to the impeller 414. This may enhance the operation of the impeller 414.
  • a baffle designed may be used to impede rotation of the liquid reaction mixture relative to the impeller 414. This may enhance the operation of the impeller 414.
  • the cooling coil and/or other structures that are integral or added to the reactor 402 may function as a baffle,
  • the cooling coil may have a serpentine shape,
  • the sensors 412 may measure one or more of the following parameters: temperature, pressure, or liquid level, The sensors 412 may be used to implement an automated control system or simply provide the operator with information about the status of the reactor 402.
  • the reactor 402 may have an emergency blowdown system as well as a gas out port.
  • the emergency blowdown system includes a large-diameter, high pressure pipe that runs from the reactor 402 to an emergency blowdown containment vessel, In the event of an emergency overheat/overpressure situation, the pipe will quickly empty the reactor 402 into the emergency blowdown containment vessel. The vessel will receive all the contents of the reactor 402 without leaking anything to the surrounding environment.
  • the gas out port is not ordinarily used to remove the gas from the reactor 402, Instead, the gas is primarily removed in the reactor effluent,
  • the reactor 402 may be any suitable size that is capable of accommodating the desired throughput.
  • the reactor 402 Once the reactor 402 reaches its start-up parameters, it is ready to begin receiving and oxidizing the primary feedstock. Shortly after the primary feedstock enters the reactor 402, the redox reaction reaches a steady operating state, At this point, the reaction mixture includes the primary feedstock, the initial start-up oxidizing acids, water, dissolved and undissolved gases as well as various reaction products, The redox reaction can be indefinitely sustained at a steady state, Although conditions in the reactor 402 may vary significantly over time, they do not vary so much that the reaction is adversely affected.
  • the start-up parameters of the reactor 402 such as the oxygen gas concentration in the headspace and the volume occupied by the reaction mixture, are maintained during operation.
  • the oxygen gas concentrations are maintained at the levels described above during operation.
  • the reaction mixture may occupy the same volume of the reactor 402 as the initial reaction mixture.
  • connection with the initial reaction mixture apply equally to the reaction mixture during operation.
  • the pressure in the reactor 402 is maintained at a level that is sufficient to keep the reaction products of nitric acid in solution so that they can react with the oxygen to regenerate the nitric acid. Sn one embodiment, the pressure in the reactor 402 is maintained at at least approximately 2070 kPa, desirably, at least approximately 2410 kPa, or, suitably, at least approximately 2800 kPa. In another embodiment, the pressure in the reactor 402 is maintained at no more than approximately 6900 kPa, desirably, no more than approximately 6200 kPa, or, suitably, no more than approximately 5515 kPa.
  • the pressure in the reactor 402 is maintained at approximately 2070 kPa to 6900 kPa, desirably, approximately 2410 kPa to 6200 kPa, or, suitably, approximately 2800 kPa to 5515 kPa. j ⁇ ll2
  • the pressure in the reactor 402 may be maintained by selectively adding the oxygen gas 406, the control gas 408, or the recycled gas 410. If the concentration of oxygen gas 406 is low, then oxygen gas 406 is added to increase the pressure. However, if additional oxygen gas 406 is not needed, then either the control gas 408 or the recycled gas 410 arc added to increase the pressure. It should be understood that the redox reaction generates gas that also contributes to the pressure inside the reactor 402. Due to the high operating pressure of the reactor 402, the oxygen gas 406, the control gas 408, and/or the recycled gas 410 may be supplied at pressures greater than 6900 kPa so that they will flow into the reactor 402.
  • the temperature of the reaction mixture is maintained at a level that prevents the nitric acid from decomposing, but encourages the rapid oxidation of the feedstock.
  • the temperature is controlled with the energy control system 416 as described above.
  • the temperature of the reaction mixture is maintained at no more than 210 0 C or, desirably, no more than 205 0 C.
  • the temperature of the reaction mixture is maintained at at least approximately 150 °C or, desirably, approximately 160 0 C.
  • the temperature of the reaction mixture is maintained at approximately 150 0 C to 210 °C or, desirably, approximately 160 °C to 205 0 C.
  • the impeller 414 is configured to disperse a sufficient amount of the oxygen gas from the headspac ⁇ into the reaction mixture to regenerate the nitric acid.
  • the oxygen reacts with the nitric acid reduction products to form nitric acid without any processing outside of the reactor.
  • the amount of the nitric acid that is regenerated can vary. In one embodiment, at least a majority of the nitric acid is regenerated, desirably, at least 75% of the nitric acid is regenerated, or, suitably at least 90% of the nitric acid is regenerated.
  • the impeller 414 circulates the gas from the headspac ⁇ through the reaction mixture so that the concentration of the gases in the reaction mixture is very similar, if not the same, as the concentration of the gases that are dissolved or undissolved in the reaction mixture.
  • concentration of dissolved and iradissoived oxygen gas in the gaseous portion of the reaction mixture is within approximately 25% of the concentration of oxygen gas in the headspace, desirably, within approximately 10% of the concentration of oxygen gas in the headspace, or, suitably, within approximately 5% of the concentration of oxygen gas in the headspace.
  • the composition of the gas in the headspace may be adjusted to control the reaction products produced by the redox reaction.
  • the desired reaction products are maximized when the composition of gases inside the reactor meet the following parameters: oxygen has the concentration given above, carbon dioxide 5% - 25% by volume; carbon monoxide 2% - 10% by volume; nitrous oxide CN 2 O) 2% - 5% by volume with the remainder being Argon and/or Nitrogen as well as minor amounts Of NO x and SO x as trace impurities.
  • the concentration of the oxidizing acids in the reaction mixture may be the same or similar to the concentration at start-up. Additional acid is added from the make-up acid source 404 as needed.
  • the feedstock undergoes a complex, exothermic, redox process.
  • the nitrogen compounds in the reaction mixture are altered so that the nitrogen compounds are reduced to gaseous nitrogen and/or nitrous oxide (N-O). Except those already listed, no compounds of the NO ⁇ type are produced in the reaction mixture at more than trace
  • a portion of the nitrogen compounds in the reaction mixture is incorporated into the complex hydrocarbons noted below.
  • a substantial portion of the carbon in the feedstock is oxidized to carbon dioxide and/or carbon monoxide. That portion of the carbon in the feedstock that is not oxidized to either carbon dioxide or carbon monoxide is incorporated into heavier hydrocarbon molecules. In situations where the oxidation potential was held to a sustained low level, a portion of the carbon in the feedstock was reduced to furanones, and furandiones, as well as other complex hydrocarbons such as paraffins.
  • the hydrogen in the reaction mixture is oxidized primary to water.
  • the hydrogen may be incorporated into complex hydrocarbons such as organic hydrofluorid.es of the type amme-dihydrofluorid ⁇ .
  • complex hydrocarbons such as organic hydrofluorid.es of the type amme-dihydrofluorid ⁇ .
  • Other minor/trace components such as phosphorous, potassium, ammonia, iron, and the like, form sulfates, nitrates, and other more complex salts.
  • a reactor effluent may be continually extracted from the reactor 402,
  • the reactor effluent primarily includes salty, acidic water (and in some embodiments, minor levels of complex hydrocarbons as noted above) since that is all that is left when the reaction is complete.
  • most, if not all, of the gas that is removed from the reactor 402 exits with the reactor effluent.
  • the gas that exits with the effluent is the dissolved and undissolvcd gas in the reaction mixture - i.e., the gaseous portion of the reaction mixture.
  • At least approximately 94 wt.% of the reaction mixture that exits the reactor 402 does so in the reactor effluent, and at least approximately 94 wt.% of the gas that exits the reactor does so in the reactor effluent.
  • at least approximately 98 wt.% of the reaction mixture that exits the reactor 402 does so in the reactor effluent, and at least approximately 98 wt.% of the gas that exits the reactor does so in the reactor effluent.
  • at least substantially all of the reaction mixture that exits the reactor 402 does so in the reactor effluent, and at least approximately substantially all of the gas that exits the reactor does so in the reactor effluent.
  • the effluent may enter the energy control system 416.
  • the energy control system 416 selves two primary functions: to extract energy from the process and to maintain the operating temperature of the reactor 402, Energy can be extracted by allowing the effluent to flow to a slightly reduced pressure heat exchanger which transfers energy to harness it for productive ends. The second function is accomplished as described above.
  • any unspent nitric acid in the reactor effluent may be removed by flashing it off before it is cooled below the boiling point of nitric acid. Also, any excess water may be flashed off in the energy control system. The need to flash or otherwise separate water from the effluent may be reduced by restricting the amount of water that is added to the feedstock.
  • FIG. 5 a block diagram of one embodiment of an effluent processing system 500 is shown.
  • the effluent processing system 500 receives the effluent after it exits the energy control system 416.
  • a number of sensors 506 are used to measure parameters such as pH and conductivity of the cooled effluent. This information may be used to control the amount of the acids 210, 212 that are added to the mixing vessel 208. For example, the lower the pH of the effluent, the less acid that needs to be added to the mixing vessel 208.
  • the cooled effluent flows to the gas separation system 502 where the pressure is allowed to drop to ambient inside the separation equipment. At this point, the effluent is vigorously agitated to drive off the dissolved and undissolvcd gases.
  • the liquid/solids stream is split with a portion of the stream going to a mixing area 510 and a portion going to the solids separation system 504, From solids separation system 504, the stream is split with part going to the mixing area 510 arid the remainder going to the waste water treatment 514. From the mixing area 510, the effluent is recycled back to the feedstock processing system 104.
  • the recycled effluent may be heated in the energy control system 416 before it reaches the feedstock processing system 104.
  • the solids recovered from the solids separation system 504 arc sent to post processing for refining into final solid products, which can are then stored, packaged, shipped and/or disposed.
  • the gases move from the gas separation system 502 through sensors 508 and on to either be recycled back to the reactor 402 or to the gas processing system 516,
  • the different gases are separated in the gas processing system 516.
  • the oxygen, plus the amounts of argon/nitrogen needed for the reactor 402 are pumped into a pressured holding lank.
  • the gases not required for the reactor 402 are processed and moved to the final gas products 518 for storing, packaging, shipping and/or disposal.
  • a method comprises: combining an initial feedstock and effluent from a reactor to form a primary feedstock; and oxidizing the primary feedstock in the reactor, the primary feedstock being part of a reaction mixture that also includes nitric acid and a secondary oxidizing acid.
  • the method may comprise comminuting the primary feedstock.
  • the method may comprise combining the initial feedstock, the effluent, and an oxidizing acid to form the primary feedstock.
  • the method may comprise combining the initial feedstock, the effluent, nitric acid, and the secondary oxidizing acid to form the primary feedstock, and wherein the concentration of nitric acid and the secondary oxidizing acid in the primary feedstock, excluding solids, may be approximately the same as the concentration of the nitric acid and the secondary oxidizing acid, respectively, in the reactor at start-up.
  • the primary feedstock may
  • the effluent may be at a temperature that is elevated relative to the ambient temperature.
  • the effluent may be acidic.
  • a method comprises: combining an initial feedstock and effluent from a reactor to form a primary feedstock; oxidizing the primary feedstock in the reactor, the primary feedstock being part of a reaction mixture that also includes nitric acid and oxygen gas; supplying the oxygen gas to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; and maintaining the reaction mixture at a temperature that is no more than approximately 210 °C.
  • the method may comprise comminuting the primary feedstock.
  • the method may comprise combining the initial feedstock, the effluent, and an oxidizing acid to form the primary feedstock.
  • the method may comprise combining the initial feedstock, the effluent, nitric acid, and a secondary oxidizing acid to form the primary feedstock, and wherein the concentration of nitric acid and the secondary oxidizing acid in the primary feedstock, excluding solids, may be approximately the same as the concentration of the nitric acid and the secondary oxidizing acid, respectively, in the reactor at start-up.
  • the primary feedstock may includes particles where the largest dimension of at least approximately 95% of the particles in the primary feedstock is no more than 4 mm.
  • the effluent may be at a temperature that is elevated relative to the ambient temperature.
  • a method comprises: combining an initial feedstock and an oxidizing acid to form a primary feedstock; oxidizing the primary feedstock in a reactor, the primary feedstock being part of a reaction mixture that also includes nitric acid and oxygen gas; supplying the oxygen gas to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; and maintaining the reaction mixture at a temperature that is no more than approximately 210 0 C.
  • the method may comprise comminuting the primary feedstock.
  • the oxidizing acid may be a primary oxidizing acid, and the method may comprise combining the initial feedstock, the primary oxidizing acid, and a secondary oxidizing acid to form the primary feedstock.
  • the concentration of the primary oxidizing acid and the secondary oxidizing acid in the primary feedstock, excluding solids, may
  • the primary feedstock may include particles where the largest dimension of at least approximately 95% of the particles in the primary feedstock is no more than 4 mm.
  • the oxidizing acid may include nitric acid.
  • a method comprises: combining an initial feedstock and effluent from a reactor to form a primary feedstock; oxidizing the primary feedstock in the reactor, the primary feedstock being part of a reaction mixture that also includes nitric acid: and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • the method may comprise comminuting the primary feedstock.
  • the method may comprise combining the initial feedstock, the effluent, and an oxidizing acid to form the primary feedstock.
  • the method may comprise combining the initial feedstock, the effluent, nitric acid, and a secondary oxidizing acid to form the primary feedstock, and wherein the concentration of nitric acid and the secondary oxidizing acid in the primary feedstock, excluding solids, may be approximately the same as the concentration of the nitric acid and the secondary oxidizing acid, respectively, in the reactor at start-up.
  • the primary feedstock may include particles where the largest dimension of at least approximately 95% of the particles in the primary feedstock is no more than 4 mm.
  • the pressure in the reactor may be at least 2800 kPa.
  • a method comprises: combining an initial feedstock and an oxidizing acid to form a primary feedstock; and oxidizing the primary feedstock in a reactor, the primary feedstock being part of a reaction mixture that also includes nitric acid and a secondary oxidizing acid.
  • a method comprises: combining an initial feedstock and an oxidizing acid to form a primary feedstock; oxidizing the primary feedstock in a reactor, the primary feedstock being part of a reaction mixture that also includes nitric acid; and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • a method comprises: combining an initial feedstock and effluent from a reactor to form a primary feedstock; oxidizing the primary feedstock in the reactor, the primary feedstock being part of a reaction mixture that also includes
  • nitric acid a secondary oxidizing acid, arid oxygen gas
  • supplying the oxygen gas to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid maintaining the reaction mixture at a temperature that is no more than approximately 210 0 C; and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • a method comprises: combining an initial feedstock and an oxidizing acid to form a primary feedstock; oxidizing the primary feedstock in a reactor, the primary feedstock being part of a reaction mixture that also includes nitric acid, a secondary oxidizing acid, and oxygen gas; supplying the oxygen gas to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; maintaining the reaction mixture at a temperature that is no more than approximately 210 0 C; and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • a method comprises: comminuting an initial feedstock to form a primary feedstock that includes particles where the largest dimension of at least approximately 95% of the particles in the primary feedstock is no more than 7 mm; oxidizing the primary feedstock in a reactor, the primary feedstock being part of a reaction mixture thai also includes nitric acid and a secondary oxidizing acid,
  • the method may comprise feeding the primary feedstock into the reactor at a feed rate that is approximately constant.
  • the method may comprises combining an oxidizing acid with the initial feedstock and/or the primary feedstock before the primary feedstock enters the reactor.
  • the method may comprise combining effluent from the reactor with the initial feedstock and/or the primary feedstock before the primary feedstock enters the reactor.
  • the initial feedstock may include effluent from the reactor.
  • the largest dimension of at least approximately 95% of the particles in the primary feedstock may be no more than 4 mm.
  • the largest dimension of at least approximately 95% of the particles in the primary feedstock may be no more than 2.5 mm.
  • the largest dimension of at least approximately 95% of the particles in the primary feedstock may be no more than 1.5 mm.
  • the largest dimension of at least approximately 95% of the particles in the primary 7 feedstock may be no more than 0.5 mm.
  • a method comprises: comminuting an initial feedstock to form a primary feedstock that includes particles where the largest dimension of at least approximately 95% of the particles in the primary feedstock is no more than 7 mm; oxidizing the primary feedstock in a reactor, the primary feedstock being part of a reaction mixture that also includes nitric acid and oxygen gas; supplying the oxygen gas to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; and maintaining the reaction mixture at a temperature that is no more than approximately 210 0 C,
  • the method may comprise combining nitric acid with the initial feedstock and/or the primary feedstock before the primary feedstock enters the reactor.
  • the method may comprise combining effluent from the reactor with the initial feedstock and/or the primary feedstock before the primary feedstock enters the reactor,
  • the initial feedstock may include effluent from the reactor,
  • the reaction mixture may include a secondary oxidizing acid.
  • the largest dimension of at least approximately 95% of the particles in the primary feedstock may be no more than 2.5 ram.
  • a method comprises: comminuting an initial feedstock to form a primary feedstock thai includes particles where the largest dimension of at least approximately 95% of the particles in the primary feedstock is no more than 7 mm; oxidizing the primary feedstock in a reactor, the primary feedstock being part of a reaction mixture that also includes nitric acid; and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • the method may comprise combining nitric acid and a secondary oxidizing acid with the initial feedstock and/or the primary feedstock before the primary feedstock enters the reactor.
  • the method may comprise combining effluent from the reactor with the initial feedstock and/or the primary feedstock before the primary feedstock enters the reactor.
  • the initial feedstock may include effluent from the reactor.
  • the largest dimension of at least approximately 95% of the particles in the primary feedstock may be no more than 2.5 mm.
  • the pressure in the reactor may be at least 2800 kPa.
  • a method comprises: comminuting an initial feedstock to form a primary feedstock that includes particles where the largest dimension of at least approximately 95% of the particles in the primary feedstock is no more than 7 mm; feeding
  • the primary feedstock into a reactor at an approximately constant feed rale; oxidizing the primary feedstock in the reactor, the primary feedstock being part of a reaction mixture that also includes nitric acid, a secondary oxidizing acid, and oxygen gas; supplying the oxygen gas to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; maintaining the reaction mixture at a temperature that is no more than approximately 210 °C; and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • the largest dimension of at least approximately 95% of the particles in the primary feedstock may be no more than 2.5 mm.
  • the initial feedstock may include effluent from the reactor.
  • The may comprise combining nitric acid and the secondary oxidizing acid with the initial feedstock and/or the primary feedstock before the primary feedstock enters the reactor.
  • the method may comprise: combining effluent from the reactor with the initial feedstock to form an intermediate feedstock: comminuting the intermediate feedstock to form a comminuted feedstock; and combining the comminuted feedstock, nitric acid, and the secondary oxidizing acid to form the primary feedstock.
  • a method comprises: feeding a feedstock into a reactor at a feed rate that is approximately constant; oxidizing the feedstock in the reactor, the feedstock being part of a reaction mixture that also includes nitric acid and a secondary oxidizing acid; and maintaining a pressure in the reactor of at least approximately 2070 kPa; wherein the feed rate is approximately constant even though the pressure in the reactor may vary from approximately 2070 kPa to 6,900 kPa.
  • the feedstock may be a slurry.
  • the slurry may include nitric acid and/or the secondary oxidizing acid.
  • the method may comprise a plurality of feeding devices that are sequentially activated and refilled to feed the feedstock into the reactor.
  • the feedstock may include particles where the largest dimension of at least approximately 95% of the particles in the feedstock is no more than 4 mm.
  • the feedstock may be fed into the reactor with a feeding device that is hydrauiicly powered.
  • the feedstock may be fed into the reactor with a feeding device that is powered by a gcarmotor.
  • a method comprises: feeding a feedstock into a reactor with a feeding device that is powered hydrauiicly or by a gearmotor; and oxidizing the
  • the method may comprise maintaining a pressure in the reactor of at least approximately 2070 kPa,
  • the feedstock may include particles where the largest dimension of at least approximately ⁇ 5% of the particles in the feedstock is no more than 4 mm.
  • the method may comprise a plurality of the feeding devices that are sequentially activated and refilled to feed the feedstock into the reactor.
  • the feedstock may include effluent from the reactor and/ or an oxidizing acid.
  • a method comprises: feeding a first amount of a feedstock into a pressurized reactor with a feeding device; isolating the feeding device from the pressurized reactor: filling the feeding device with a second amount of the feedstock; feeding the second amount of the feedstock into the pressurized reactor with the feeding device; oxidizing the feedstock in the pressurized reactor, the feedstock being part of a reaction mixture that also includes nitric acid and a secondary oxidizing acid; and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • the method may comprise a valve that isolates the feeding device from the pressurized reactor,
  • the first amount of the feedstock and the second amount of the feedstock may be fed into the pressurized reactor at a feed rate that is approximately constant.
  • Filling the feeding device with the second amount of the feedstock may be done at a pressure that is greatly reduced from the pressure of the pressurized reactor.
  • the pressure in the reactor may be at least 2800 kPa.
  • a method comprises: feeding a feedstock into a reactor at a feed rate that is approximately constant; oxidizing the feedstock in the reactor, the feedstock being part of a reaction mixture that also includes nitric acid, a secondary oxidizing acid, and oxygen gas; supplying the oxygen gas to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; maintaining the reaction mixture at a temperature that is no more than approximately 2H) 0 C; and maintaining a pressure in the reactor of at least approximately 2070 kPa; wherein the feed rate is approximately constant even though the pressure in the reactor may vary from approximately 2070 kPa to 6,900 kPa.
  • the feedstock may include particles where the largest dimension of at least approximately 95% of the particles
  • the method may comprise a plurality of feeding devices that are sequentially activated and refilled to feed the feedstock into the reactor.
  • the feedstock may include effluent from the reactor and/or an oxidizing acid.
  • a method comprises: feeding a feedstock into a reactor at a feed rate that fluctuates no more than approximately 10% per hour; oxidizing the feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid; and maintaining a pressure in the reactor of at least approximately 2070 kPa; wherein the feed rate fluctuates no more than approximately 10% per hour even though the pressure in the reactor may vary from approximately 2070 kPa to 6,900 kPa.
  • a method comprises: feeding a feedstock into a reactor with a feeding device that is powered hydraulic Iy or by a gearraotor; oxidizing the feedstock in the reactor, the feedstock being part of a reaction mixture that also includes nitric acid and oxygen gas: supplying the oxygen gas to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; and maintaining the reaction mixture at a temperature that is no more than approximately 210 0 C.
  • a method comprises: feeding a feedstock into a reactor with a feeding device that is powered hydraulicly or by a gearraotor; oxidizing the feedstock in the reactor, the feedstock being part of a reaction mixture that also includes nitric acid; and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • a method comprises: feeding a feedstock into a reactor with a feeding device that is powered hydraulicly or by a gearmotor; oxidizing the feedstock in the reactor, the feedstock being part of a reaction mixture that also includes nitric acid, a secondary oxidizing acid, and oxygen gas: supplying the oxygen gas to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; maintaining the reaction mixture at a temperature that is no more than approximately 210 °C; and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • a method comprises: feeding a first amount of a feedstock into a pressurized reactor with a feeding device; isolating the feeding device from the
  • pressurized reactor filling the feeding device with a second amount of the feedstock; feeding the second amount of the feedstock into the pressurized reactor with the feeding device; oxidizing the feedstock in the pressurized reactor, the feedstock being part of a reaction mixture that also includes nitric acid; and maintaining a pressure in the pressurized reactor of at least approximately 2070 kPa; wherein the first amount of the feedstock and the second amount of the feedstock are fed into the pressurized reactor at a feed rate that fluctuates no more than approximately 10% per hour;
  • a method comprises: feeding a first amount of a feedstock into a pressurized reactor with a feeding device; isolating the feeding device from the pressurized reactor; filling the feeding device with a second amount of the feedstock; feeding the second amount of the feedstock into the pressurized reactor with the feeding device; oxidizing the feedstock in the pressurized reactor, the feedstock being part of a reaction mixture that also includes nitric acid, a secondary oxidizing acid, and oxygen gas; supplying the oxygen gas to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; maintaining the reaction mixture at a temperature that is no more than approximately 210 0 C; and maintaining a pressure in the reactor of at least approximately 2070 kPa; wherein the first amount of the feedstock and the second amount of the feedstock are fed into the pressurized reactor at a feed rate that is approximately constant;
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid and a secondary oxidizing acid; and dispersing gas from a headspace of the reactor into the reaction mixture.
  • the method may comprise dispersing the gas from the headspace into the reaction mixture with an impeller that is hollow and causes gas from the headspace to flow through the impeller into the reaction mixture.
  • the method may comprise dispersing the gas from the headspace into the reaction mixture with a gas entrainment impeller.
  • the method may comprise supplying oxygen gas to the reactor and dispersing the oxygen gas from the headspace of the reactor into the reaction mixture.
  • the method may comprise a baffle positioned in the reaction mixture to enhance the dispersion of the gas from the headspace into the reaction mixture.
  • the method may comprise maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • the gas in the headspace may include 2 to 60 volume percent oxygen gas.
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid and oxygen gas: supplying the oxygen gas to the reactor; dispersing the oxygen gas from a headspace of the reactor into the reaction mixture in a mariner that is sufficient to regenerate at least a majority of the nitric acid; and maintaining the reaction mixture at a temperature that is no more than approximately 210 °C.
  • the gas in the headspace may include 2 to 60 volume percent oxygen gas.
  • the method may comprise dispersing the gas from the headspace into the reaction mixture with an impeller that is hollow and causes gas from the headspace to ilow through the impeller into the reaction mixture.
  • the method may comprise dispersing the gas from the headspace into the reaction mixture with a gas entrainm ⁇ nt impeller.
  • the method may comprise maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid and a secondary oxidizing acid; and maintaining the concentration of dissolved and undissolved oxygen gas in the gaseous portion of the reaction mixture within approximately 25% of the concentration of oxygen gas in a headspace of the reactor.
  • the method may comprise maintaining the concentration of dissolved and undissolved oxygen gas in the gaseous portion of the reaction mixture within approximately 10% of the concentration of oxygen gas in the headspace of the reactor.
  • the method may comprise maintaining the concentration of dissolved and undissolved oxygen gas in the gaseous portion of the reaction mixture within approximately 5% of the concentration of oxygen gas in the headspace of the reactor.
  • the method may comprise dispersing the oxygen gas from the headspace into the reaction mixture with a gas entrainment impeller.
  • the headspace may include 2 to 60 volume percent oxygen gas.
  • the headspace may include 5 to 45 volume percent oxygen gas,
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid, a secondary
  • the method may comprise maintaining the concentration of dissolved and undissolved oxygen gas in the gaseous portion of the reaction mixture within approximately 10% of the concentration of oxygen gas in the headspacc of the reactor.
  • the method may comprise dispersing the oxygen gas from the headspace into the reaction mixture with an impeller that is hollow and causes the oxygen gas from the headspace to flow through the impeller into the reaction mixture.
  • the method may comprise dispersing the oxygen gas from the headspace into the reaction mixture with a gas entrainment impeller.
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid; dispersing gas from a headspace of the reactor into the reaction mixture: and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid and oxygen gas; supplying the oxygen gas to the reactor mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; maintaining the concentration of dissolved and undissolved oxygen gas in the gaseous portion of the reaction mixture within approximately 25% of the concentration of oxygen gas in a headspace of the reactor; and maintaining the reaction mixture at a temperature that is no more than approximately 210 0 C.
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid; maintaining the concentration of dissolved and undissolved oxygen gas in the gaseous portion of the reaction mixture within approximately 25% of the concentration of oxygen gas in a headspace of the reactor; and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid, a secondary oxidizing acid, and oxygen gas; supplying the oxygen gas to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; maintaining the concentration of dissolved and undissolved oxygen gas in the gaseous portion of the reaction mixture within approximately 25% of the concentration of oxygen gas in a headspace of the reactor; maintaining the reaction mixture at a temperature that is no more than approximately 210 0 C; and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid and a secondary oxidizing acid; supplying gas to the reactor; and removing a reactor effluent from the reactor; wherein at least approximately 94 wt.% of the reaction mixture that exits the reactor does so in the reactor effluent; and wherein at least approximately 94 wl.% of gas that exits the reactor does so in the reactor effluent,
  • the method may comprise dispersing gas from a headspace of the reactor into the reaction mixture.
  • the method wherein at least approximately 98 wt.% of the reaction mixture that exits the reactor does so in the reactor effluent; and wherein at least approximately 98 wt.% of gas that exits the reactor does so in the reactor effluent.
  • the method may comprise separating the gas from the reactor effluent.
  • the method may comprise combining the feedstock with at least a portion of the reactor effluent.
  • a headspace of the reactor may include 5 to 45 volume percent oxygen gas.
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid and oxygen gas; supplying gas to the reactor, the supplied gas including the oxygen gas; removing a reactor effluent from the reactor; and maintaining the reaction mixture at a temperature that is no more than approximately 210 0 C; wherein the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; wherein at least approximately 94 wt.% of the reaction mixture that exits the reactor does so in the reactor effluent; and wherein at least approximately 94 wt.% of gas that exits the reactor does so in the
  • the method may comprise dispersing the oxygen gas from a headspace of the reactor into the reaction mixture.
  • a headspace of the reactor may include 5 to 45 volume percent oxygen gas.
  • the method may comprise combining the feedstock with at least a portion of the reactor effluent.
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid and a secondary oxidizing acid; supplying oxygen gas to the reactor; removing a reactor effluent from the reactor; measuring the amount of oxygen gas in the reactor effluent: and adjusting the supply of oxygen gas to the reactor based on the amount of oxygen gas measured in the reactor effluent.
  • the method may comprise dispersing the oxygen gas from a headspace of the reactor into the reaction mixture.
  • the method may comprise maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • the method may comprise supplying inert gas to the reactor to maintain the pressure of at least approximately 2070 kPa.
  • a headspace of the reactor may include 2 to 60 volume percent oxygen gas.
  • a headspace of the reactor may include 5 to 45 volume percent oxygen gas,
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid, a secondary oxidizing acid, and oxygen gas; supplying gas to the reactor, the supplied gas including the oxygen gas; removing a reactor effluent from the reactor: maintaining the reaction mixture at a temperature that is no more than approximately 210 0 C; and maintaining a pressure in the reactor of at least approximately 2070 kPa; wherein the oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid; wherein at least approximately 94 wt.% of the reaction mixture that exits the reactor does so in the reactor effluent: and wherein at least approximately 94 wt.% of gas that exits the reactor docs so in the reactor effluent.
  • the method may comprise dispersing the oxygen gas from a headspace of the reactor into the reaction mixture.
  • the method may comprise cooling the reactor effluent;
  • a headspace of the reactor may include 5 to 45 volume percent oxygen gas.
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid; supplying gas to the reactor; removing a reactor effluent from the reactor; and maintaining a pressure in the reactor of at least approximately 2070 kPa; wherein at least approximately 94 wt.% of the reaction mixture that exits the reactor does so in the reactor effluent; and wherein at least approximately 94 wt.% of gas that exits the reactor docs so in the reactor effluent.
  • a method comprises: oxidizing a feedstock m a reactor, the feedstock being part of a reaction mixture that also includes nitric acid and oxygen gas; supplying the oxygen gas to the reactor in an amount that is sufficient to regenerate at least a majority of the nitric acid; removing a reactor effluent from the reactor; measuring the amount of oxygen gas in the reactor effluent; adjusting the supply of oxygen gas to the reactor based on the amount of oxygen gas measured in the reactor effluent; and maintaining the reaction mixture at a temperature that is no more than approximately 210 °C.
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid; supplying oxygen gas to the reactor; removing a reactor effluent from the reactor; measuring the amount of oxygen gas in the reactor effluent; adjusting the supply of oxygen gas to the reactor based on the amount of oxygen gas measured in the reactor effluent; and maintaining a pressure in the reactor of at least approximately 2070 kPa.
  • a method comprises: oxidizing a feedstock in a reactor, the feedstock being part of a reaction mixture that also includes nitric acid, a secondary oxidizing acid, and oxygen gas; supplying oxygen gas to the reactor; removing a reactor effluent from the reactor; measuring the amount of oxygen gas in the reactor effluent; adjusting the supply of oxygen gas to the reactor based on the amount of oxygen gas measured in the reactor effluent; maintaining the reaction mixture at a temperature that is no more than approximately 210 0 C; and maintaining a pressure in the reactor of at least approximately 2070 kPa; wherein the
  • oxygen gas is supplied to the reaction mixture in an amount that is sufficient to regenerate at least a majority of the nitric acid.
  • a stated range of 1 to 10 should be considered to include and provide support for claims that recite any and all subranges or individual values that are between and/or inclusive of the minimum value of 1 and the maximum value of 10: that is, all subranges beginning with a minimum value of 1 or more and ending with a maximum value of 10 or less (e.g., 5.5 to 10, 2,34 to 3.56, and so forth) or any values from 1 to 10 (e.g., 3, 5.8, 9.9994, and so forth).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Water Supply & Treatment (AREA)
  • Engineering & Computer Science (AREA)
  • Hydrology & Water Resources (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Treatment Of Sludge (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)
  • Fertilizers (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Processing Of Solid Wastes (AREA)
EP10711122A 2009-04-01 2010-03-23 Improved aqueous phase oxidation process Withdrawn EP2414097A2 (en)

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
US12/416,412 US7951988B2 (en) 2009-04-01 2009-04-01 Aqueous phase oxidation process
US12/416,424 US7915474B2 (en) 2009-04-01 2009-04-01 Aqueous phase oxidation process
US12/416,419 US8115047B2 (en) 2009-04-01 2009-04-01 Aqueous phase oxidation process
US12/416,431 US8481800B2 (en) 2009-04-01 2009-04-01 Aqueous phase oxidation process
US12/416,438 US8168847B2 (en) 2009-04-01 2009-04-01 Aqueous phase oxidation process
PCT/US2010/028340 WO2010120450A2 (en) 2009-04-01 2010-03-23 Improved aqueous phase oxidation process

Publications (1)

Publication Number Publication Date
EP2414097A2 true EP2414097A2 (en) 2012-02-08

Family

ID=42199039

Family Applications (1)

Application Number Title Priority Date Filing Date
EP10711122A Withdrawn EP2414097A2 (en) 2009-04-01 2010-03-23 Improved aqueous phase oxidation process

Country Status (8)

Country Link
EP (1) EP2414097A2 (zh)
JP (3) JP2012522635A (zh)
KR (1) KR20120013957A (zh)
CN (1) CN102438741A (zh)
CA (1) CA2756772C (zh)
CL (1) CL2011002413A1 (zh)
MX (1) MX2011010357A (zh)
WO (1) WO2010120450A2 (zh)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP6238116B2 (ja) * 2012-12-04 2017-11-29 株式会社リコー 流体浄化装置
CN110921901A (zh) * 2019-12-07 2020-03-27 衡水均凯化工有限公司 一种碱性废液的处理方法

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2916203A1 (de) * 1979-04-21 1980-11-06 K E W A Kernbrennstoff Wiedera Verfahren zur behandlung von brennbaren, festen, radioaktiven abfaellen
US4350599A (en) * 1980-12-29 1982-09-21 Sterling Drug Inc. Process for treatment of caustic waste liquors
MX171672B (es) * 1988-07-19 1993-11-10 Safe Waste Systems Inc Composicion para encapsular cromo, arsenico y otros metales toxicos presentes en desechos y procedimiento para tratar los mismos
EP0568736A1 (en) * 1992-05-06 1993-11-10 WASTE TREATMENT PATENTS & RESEARCH N.V. Method for co-processing organic wastes and spent nitric acid wash water
CZ282553B6 (cs) * 1993-01-27 1997-08-13 R & O Mining Processing Ltd. Hydrometalurgické znovuzískávání kovů z komplexních rud
US5785868A (en) * 1995-09-11 1998-07-28 Board Of Regents, Univ. Of Texas System Method for selective separation of products at hydrothermal conditions
JPH1043710A (ja) * 1996-08-02 1998-02-17 Hitachi Ltd 金属酸化物および被酸化性物質を含む廃棄物の処理方法およびその処理装置
JPH10146574A (ja) * 1996-11-20 1998-06-02 Mitsubishi Materials Corp 飛灰の処理方法
US5814292A (en) * 1996-12-19 1998-09-29 Energy Research Group Comprehensive energy producing methods for aqueous phase oxidation
CN1213097C (zh) * 1997-08-20 2005-08-03 东芝株式会社 废弃物处理方法和废弃物处理装置
SE518803C2 (sv) * 1999-09-03 2002-11-26 Chematur Eng Ab Metod och reaktionssystem med högt tryck och hög temperatur som är lämpat för superkritisk vattenoxidation
JP2002045823A (ja) * 2000-08-07 2002-02-12 Shiro Yoshizaki 重金属類除去方法
JP2003299941A (ja) * 2002-04-04 2003-10-21 Kurita Water Ind Ltd 水熱酸化反応処理装置および方法
CN1232662C (zh) * 2002-09-03 2005-12-21 福州大学 一种从工业废渣中提取钴的方法

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
None *
See also references of WO2010120450A2 *

Also Published As

Publication number Publication date
CL2011002413A1 (es) 2012-06-15
WO2010120450A3 (en) 2011-01-20
CA2756772C (en) 2017-09-26
WO2010120450A2 (en) 2010-10-21
AU2010236942A1 (en) 2011-10-27
JP2016106023A (ja) 2016-06-16
CA2756772A1 (en) 2010-10-21
JP2012522635A (ja) 2012-09-27
JP2014144452A (ja) 2014-08-14
MX2011010357A (es) 2011-12-16
CN102438741A (zh) 2012-05-02
KR20120013957A (ko) 2012-02-15

Similar Documents

Publication Publication Date Title
US8481800B2 (en) Aqueous phase oxidation process
EP2632863B1 (en) Waste treatment process
US7951988B2 (en) Aqueous phase oxidation process
CN101716450B (zh) 一种除氧复合药剂/uv联用的除氧方法
US20070090057A1 (en) Process for the purification of acidic metal-bearing waste waters to permissable discharge levels with recovery of marketable metal products
US9902632B2 (en) Waste treatment method
US8115047B2 (en) Aqueous phase oxidation process
US8168847B2 (en) Aqueous phase oxidation process
US7915474B2 (en) Aqueous phase oxidation process
CN107572687A (zh) 一种染料/涂料废水的处理方法
CA2756772C (en) Improved aqueous phase oxidation process
CN102452763A (zh) 一种乙烯废碱液的处理方法
CN202400887U (zh) 一种三维粒子电解催化氧化污水处理装置
Zhu et al. Synergetic interaction of lithium cobalt oxide with sulfite to accelerate the degradation of organic aqueous pollutants
AU2010236942B2 (en) Improved aqueous phase oxidation process
KR101199023B1 (ko) 영가철 제조장치 및 이를 이용한 영가철의 제조방법
CN107572688A (zh) 一种有机废碱液处理装置和方法
Chang et al. Selective granulation of trivalent iron into ferric hydroxide from bi-metal containing wastewater using Fluidized-Bed Homogeneous Crystallization technology
Farshi et al. Kinetic study for oxidation of existing mercaptans in kerosene using impregnated activated carbon with MEROX catalyst in alkaline solution
BRPI1014860A2 (pt) processo aperfeiçoado para oxidação de fase aquosa
CN207375866U (zh) 一种芬顿氧化处理装置
EP2969975A1 (en) pH CONTROL TO ENABLE HOMOGENEOUS CATALYTIC WET AIR OXIDATION
Lin et al. Enhanced precipitation of CaMoO4 for continuous recovery of molybdenum from Mo-contained wastewater and application to fluidized bed homogeneous crystallization
Li et al. Notice of Retraction: Treatment of oily wastewater generated from steel production by supercritical water oxidation
Sun et al. Absorption of NO into aqueous coal slurry with added FeII (EDTA) in the presence of SO2

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20111018

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR

DAX Request for extension of the european patent (deleted)
17Q First examination report despatched

Effective date: 20131029

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20180213